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EP0273723A2 - Trennung eines mit Sauerstoff angereicherten Gases - Google Patents

Trennung eines mit Sauerstoff angereicherten Gases Download PDF

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Publication number
EP0273723A2
EP0273723A2 EP87311411A EP87311411A EP0273723A2 EP 0273723 A2 EP0273723 A2 EP 0273723A2 EP 87311411 A EP87311411 A EP 87311411A EP 87311411 A EP87311411 A EP 87311411A EP 0273723 A2 EP0273723 A2 EP 0273723A2
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EP
European Patent Office
Prior art keywords
column
gas
feed
pressure
completed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP87311411A
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English (en)
French (fr)
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EP0273723A3 (de
Inventor
Taichi Tagawa
Yasuto Suzu
Shigeki Hayashi
Yasumitsu Mizuguchi
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Osaka Oxygen Industries Ltd
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Osaka Oxygen Industries Ltd
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Publication date
Application filed by Osaka Oxygen Industries Ltd filed Critical Osaka Oxygen Industries Ltd
Publication of EP0273723A2 publication Critical patent/EP0273723A2/de
Publication of EP0273723A3 publication Critical patent/EP0273723A3/de
Withdrawn legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0476—Vacuum pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0473—Rapid pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/30—Physical properties of adsorbents
    • B01D2253/302—Dimensions
    • B01D2253/304—Linear dimensions, e.g. particle shape, diameter
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/102—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40013—Pressurization
    • B01D2259/40015—Pressurization with two sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40028—Depressurization
    • B01D2259/40032—Depressurization with three sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40067—Seven
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/403—Further details for adsorption processes and devices using three beds

Definitions

  • the present invention relates to a process for separating a gas enriched oxygen from air through pressure swing adsorption by using an adsorbent which is capable of selectively adsorbing nitrogen.
  • Pressurization is effected with the product gas, and afterwards the feed end of the column and the effluent end of the column after adsorption has been completed are connected together for pressure equalization, thereby advantageously realizing a high rate of recovery of oxygen and an increased amount of oxygen produced per unit amount of adsorbent (hereinafter referred to as "specific product").
  • specific product adsorbent
  • a group of recent applications i.e., Japanese Patent Public Disclosure Nos. 60-161308 (161308/1985), 60-161309 (161309/1985), 61-133114 (133114/1986) and 61-133115 (133115/1986), utilize evacuation to lower the adsorption pressure and improve the specific power consumption and the rate of recovery of oxygen, but have not yet overcome all of the above-described disadvantages.
  • these applications are basically analogous processes, that is, the supply of the feed gas is suspended before all the adsorbent is charged with impurity.
  • the specific product is reduced and, at the same time, it is disadvantageously necessary to effect complicated and time consuming adjustment thereafter for lowering the pressure utilized for pressure equalization and purging.
  • Japanese Patent Public Disclosure No. 60-180903 (180903/1985) discloses a process which includes adsorption, evacuation and pressurization by a product gas. However, it is stated that, if purging by a product gas is not also used, the specific product falls and the specific power consumption rises.
  • a process for producing an enriched oxygen gas having a lowered nitrogen content is disclosed in Japanese Patent Public Disclosure No. 48-83078 (83078/1973). It is stated, however, that oxygen enriched gas cannot be obtained by a three-column system, and one example is given in which the nitrogen content was lowered from 0.27% to 160 ppm in a four-column system. However, since the specific product is considerably low, this process is considered economically impractical. Thus, there has heretofore been no oxygen enriching technique which enables production of an oxygen gas having a lowered nitrogen content while being satisfactory in terms of specific power consumption, specific product and rate of recovery.
  • the present process separates oxygen from a feed gas containing at least oxygen, nitrogen and argon by pressure swing adsorption using three adsorption columns containing an adsorbent capable of selective adsorption of nitrogen which comprises repeatedly performing the steps of:
  • FIGS. 1A to 1C are flow sheets showing a process in which a gas enriched in oxygen is continuously generated from air.
  • Each of the three adsorption columns A, B and C contains an adsorbent capable of selectively adsorbing nitrogen. Control of each of the steps can be regulated by conventional means, e.g. a timer.
  • valves 1a and 2A are opened and air, pressurized by a blower 9, is introduced to the first column A from its lower or feed end, thus causing the product gas (O2 and Ar) therein to be withdrawn from the upper effluent end and introduced into a tank 11 through a line 12.
  • the pressure in the first column A is normally maintained above atmospheric pressure up to 0.5 kg/cm2G, preferably, from about 0.1 to 0.35 kg/cm2G.
  • valves 3B and 5B are open and oxygen enriched gas is supplied from the effluent end of the third column C to the effluent end of the second column B.
  • This oxygen enriched gas is discharged to the outside of the system by means of a vacuum pump 10 after purging the inside of the second column B counter-currently to the direction of flow of the feed gas.
  • the third column C is thus depressurized while the oxygen enriched gas is supplied therefrom to the second column B.
  • the rate of supply of the oxygen enriched gas from the third column C is controlled by means of a flow control valve 6B.
  • valves 3B and 5B are closed and valves 4B and 3C are opened.
  • Product gas is introduced from the tank 11 through line 13 to the effluent end of the second column B, which had been purged, to pressurize it.
  • the first column A continuously produces product gas from the effluent end while the third column C is evacuated by means of vacuum pump 10.
  • the pressurization of the second column B can be conducted by means other than the supply of the product gas from the tank 11 as described above.
  • part of the product gas from the first column A is introduced to the second column B. through the line 13 and the valve 4B after the flow rate thereof has been adjusted by means of a valve 7.
  • FIG. 1B part of the product gas from the first column A is introduced to the second column B. through the line 13 and the valve 4B after the flow rate thereof has been adjusted by means of a valve 7.
  • FIG. 1B part of the product gas from the first column A is introduced to the second column B. through the line 13 and the valve 4B after the flow rate thereof has been
  • part of the product gas from the first column A is introduced in to the second column B through valves 5A and 6A after the flow rate thereof has been adjusted by the valve 6A.
  • the line 13 and the valves 4A, 4B and 4C are not needed.
  • valves 2A and 4B are closed and valve 1B is opened thereby causing gas within the first column A, to flow from the feed end of the first column A to the feed end of the second column B, thus countercurrently depressurizing column A, while the feed air is now passed to the second column B.
  • valves 2A and 2B may be open to introduce the oxygen enriched gas from the effluent end of the column A to the effluent end of the column B.
  • Step 3 is typically carried out for about 1 to 7 seconds.
  • depressurization is effected only by introducing gas from the feed end of the column A to the feed end of the column B
  • the above described operation is preferably carried out for about 3 to 5 seconds.
  • gas is introduced from the effluent end of the column A to the effluent end of the column B simultaneously with the above-described depressurization, the operation is preferably carried out for only about 1 to 2 second.
  • valve 1A is closed, and valve 5C is opened causing oxygen enriched gas to flow from the effluent end of the column A to the effluent end of column C.
  • Column C is purged countercurrently to the direction of flow of feed gas, the gas being vented from the system by the operation of vacuum pump 10.
  • the first column A is thus further depressurized while introducing the oxygen enriched gas to the third column C.
  • the rate of supply of the purge gas from the column A to column C is controlled by means of a flow control valve 6C.
  • the rate of supply of the purge gas is not critical. The rate of supply of the purge gas may be determined by the final pressure within the column which is depressurized to supply the purge gas.
  • the final pressure within the first column A is normally set at from -6 cmHg to 0.1 kg/cm2G, preferably near atmospheric pressure.
  • the valve 2B is kept open so that product gas is flowing from the effluent end of the second column B.
  • the fifth step is carried out at a pressure of from about 250 to 350 Torr, preferably from about 270 to 330 Torr.
  • valves 2B and 4C are closed and valve 1C is opened to introduce the gas from the feed end of column B to the feed end of column C, together with the feed air, thereby depressurizing column B.
  • valves 2B and 2C may be opened to introduce enriched oxygen gas from the effluent end of column B to the effluent end of column C.
  • Column A is continuously evacuated during this period.
  • valve 1B is closed and valve 5A is opened thereby introducing oxygen enriched gas from the effluent end of column A while purging column A countercurrently. This gas is vented from the system by the vacuum pump 10.
  • the step 6 may be carried out after the completion of the step 5 or vice versa. Alternatively, after the evacuation in step 5 has been completed, the purging in step 6 is carried out, and then evacuation is resumed.
  • both the values 1C and 2C may remain open, so that product gas flows out from the effluent end of column C.
  • valves 3A and 5A are closed and valve 4A is opened to introduce the product gas from the tank 11 to the effluent end of column A which has been purged, thereby pressurizing column A with product gas.
  • the rate of introduction of the product gas is controlled by flow control value 7.
  • the pressurization by the product gas is essential for stably obtaining a product gas of low nitrogen concentration (e.g., about 1000ppm) for the following reasons.
  • the pressure within column A at the end of the pressurization step (7) is preferably from about 250 to 450 Torr higher than the pressure at the end of the purging step 6.
  • valve 3B is open and column B is evacuated by operation of the vacuum pump 10 while column C continuously receiving feed gas (air), with the withdrawal of product gas out from the effluent end thereof.
  • valves 2C and 4A are closed and valve 1A is opened to introduce gas from the feed end of the column C to the feed end of column A, together with the feed air, thereby pressurizing column A.
  • column C is supplied with air from its feed end and separates nitrogen therefrom discharging an oxygen enriched gas from its effluent end.
  • the adsorbing step (step 7) is completed.
  • a relatively large amount of oxygen enriched gas the concentration of which is lower than the oxygen concentration in the product gas but still considerably higher than the concentration of oxygen in air is left in the gaseous portion at the effluent end of column C.
  • step 8 is effected within a short period of time, i.e., from about 1 to 7 seconds, preferably from about 3 to 5 seconds.
  • valves 2C and 2A may be open to introduce the oxygen enriched gas from the effluent end of column C to the effluent end of column A, thereby pressurizing column A.
  • the purpose of the alternative operation is to recover the oxygen enriched gas, that remains in the gaseous phase at the effluent end of column C at the end of step 7 .
  • the oxygen concentration of this gas is close to that of the product gas recovered from the effluent end of column A.
  • the pressure within column A is raised by introducing the gas from both the feed and effluent ends of column C to both the feed and effluent ends of column A, the pressure within column C will lower at approximately double the speed in comparison to the introduction of gas from only the feed end of column C to the feed end of column A. Therefore, it is possible to effect the operation within a shorter period of time, e.g., from 1 to 2 seconds. Accordingly, there is substantially no desorption of nitrogen from the adsorbent layer to the gaseous phase in column C.
  • the flow is periodically switched among the above-described adsorption columns so as to repeat the above steps on a cyclic basis.
  • the product gas is continuously taken out from the tank 11 through valve 8.
  • the present invention enables air to be enriched in oxygen and efficiently taken out as a product gas by the adsorption of nitrogen from air. More specifically, it is possible according to the present invention to increase the specific product by effectively shifting the break-through front of nitrogen adsorption to the effluent end, i.e. the downstream end, of each adsorption column during its adsorption step. It is also possible to reduce the required amount of feed gas by passing residual unadsorbed gas at the end of an adsorption step, to another column for recovery. Further, it is possible to lower the adsorption pressure and raise the vacuum pressure by the combination of purging and pressurization of the adsorbent beds by the product gas. Thus, it is possible to provide a process for readily obtaining an oxygen enriched gas having a reduced nitrogen content at a lowered specific power consumption and an increased specific product.
  • pressure swing adsorption pressurization and depressurization are alternately repeated and separation of the gas mixture is made possible by the difference between the adsorbed gas content and the desorbed gas content.
  • Methods for carrying out pressure swing adsorption may roughly be divided into three types: a first type utilizing compression to a pressure above atmospheric pressure i.e., the pressure employed therein ranges from a positive pressure to a sub-atmospheric pressure; a second type in which the pressure never falls below atmospheric pressure; a third type in which the pressure never rises above atmospheric pressure.
  • the theoretical power consumption in pressure swing adsorption is calculated on the basis of the compression ratio employed to attain a pressure more than atmospheric pressure, or that employed to raise the pressure from a sub-atmospheric pressure to atmospheric pressure.
  • the first type of process has the lowest compression ratio. Since the power consumption falls as the compression ratio decreases, the specific power consumption is minimized by adopting methods of the first type.
  • a substantially constant pressure in step 2 is maintained of which is typically higher than atmospheric pressure, i.e., 0.5 kg/cm2G, preferably from about 0.1 to 0.35 kg/cm2G, and the ultimate pressure by evacuation (hereinafter referred to as "evacuate pressure") in the steps 5-1 and 5-2 is typically from about 250 to 350 Torr, preferably within the range of 300 Torr ⁇ 30 Torr. Since in step 6 the purge gas is introduced during evacuation, the evacuate pressure is normally 10 to 50 Torr higher than that in the step 5-2, and it is therefore possible to further reduce the power consumption by the vacuum pump.
  • a first feature of the present invention is that it provides a method of recovering residual unadsorbed gas from each adsorption column at the end of adsorption by passing the gas to another column which has been regenerated by pressurization with product gas in step 7. This passage of gas is continued until the pressures in the two columns have been substantially equalised.
  • the passage of the gas during pressure equalization may be effected by one of the following three methods: (a) the gas is passed from the effluent end of one column to the feed end of another column; (b) the gas is passed from the effluent end of the former to the effluent end of the latter; and (c) the gas is passed from the feed end of the former to the feed end of the latter.
  • the three methods if the average oxygen concentration in the recovered gas is equal to or higher than the oxygen concentration in the feed gas, the compression of the feed gas can be reduced, so that it is possible to increase the rate of recovery and lower the specific power consumption.
  • pressure equalization is effected between the feed ends of two columns, that is , the method (c) is employed.
  • an adsorption column which is depressurized after the completion of the adsorption step has the gas passed therethrough countercurrently to the direction of air flow and, therefore, there is no possibility that its effluent end will be contaminated by nitrogen gas. Accordingly, it is possible to shift satisfactorily the break-through front of nitrogen adsorption to the effluent end of the adsorption column, even in the adsorption step. As a result, it is possible to generate a product gas having a lowered nitrogen concentration at a high specific product.
  • gas is simultaneously passed from the feed end of one column to the feed end of another (i.e., the first case), while gas is also moved from the effluent end of the former to the effluent end of the latter.
  • Pressure equalization in which the gas is passed from one column to another is therefore carried out simultaneously with introduction of the feed gas into the lower pressure column until the pressures within the two columns become substantially equal.
  • the recovered gas is unadsorbed gas taken from the gaseous phase present in the void spaces in the adsorbent column and, therefore, it is particularly preferable to complete pressure equalisation before the nitrogen adsorbed in the solid phase is desorbed therefrom.
  • the object of this operation is to recover only the gas which is present within the void portions in the adsorption column and adsorbed argon and oxygen which are relatively easy to desorb from the adsorbent. Accordingly it was possible in the first embodiment to reduce the pressure difference between the two columns to 0.01 kg/cm2 within about 1 to 7 seconds, preferably about 3 or 5 seconds, and in the second embodiment, it was possible to reduce the pressure difference to 0.01 kg/cm2 within about 1 to 3 seconds, preferably about 1 to 2 seconds. Thus, it is possible to make the pressures within the two columns substantially equal within a favorably short period of time.
  • FIG. 7 is a graph showing the relationship between the nitrogen concentration and the specific product
  • the specific product decrease at a relatively low rate to a nitrogen concentration of about 0.05% (500 ppm) and, as the nitrogen concentration is further lowered, the specific product rapidly decreases.
  • FIG. 8 is a graph showing the relationship between the specific power consumption and the nitrogen concentration.
  • the specific power consumption rises at a very low rate to a nitrogen concentration of about 0.05% (500ppm), and as the nitrogen concentration is further lowered, the specific power consumption rapidly rises.
  • the process of the present invention has the capacity to produce an enriched oxygen gas having a nitrogen concentration of from about 500 ppm to 1.0%.
  • the purge gas utilized in step 4 of the method of the present invention is a gas present in a column from which the adsorbed gas has already been recovered by pressure equalization and which gas has a lower oxygen concentration than that of the product gas, i.e., about 70 to 90%.
  • This gas is, therefore, effectively employed for purging nitrogen from the adsorbent.
  • the purging operation is effected by depressurizing the column which is to be supplied with the purge gas to a pressure near atmospheric pressure for from about 12 to 20 seconds in the case where the part cycle time is 60 seconds.
  • step 7 It is essential to use part of the product gas for pressurization in step 7 in order to obtain an oxygen enriched gas of high concentration and in particular, to generate a product gas having a low nitrogen concentration.
  • the product gas backfill pressure is increased, the specific product of the oxygen enriched gas having a low nitrogen concentration increases.
  • step 2 when the product gas backfill pressure is excessively increased, the specific product increases, but the flow velocity of the feed gas within the column in the adsorption step (step 2) increases to lower the adsorption - desorption efficiency, and this leads to a lowering in the rate of recovery, resulting in an increase in the specific power consumption.
  • step 2 when the product gas backfill pressure is excessibly lowered, the specific product rapidly decreases to increase the specific power consumption. Accordingly, it is not desirable to lower substantially the product gas backfill pressure or omit this pressurizing operation.
  • the process of the present invention can readily and economically be practised stably to generate a product gas having a low nitrogen content, i.e., 1.0%, or 0.5%, or even 0.1% or less, which has not heretofore been achieved.
  • the process of the present invention makes possible generation of an enriched oxygen gas having a high oxygen concentration, i.e., at least 85%, typically 90% to 93% or more, which are equal to those heretofore achieved.
  • the oxygen concentration and the specific power consumption have heretofore been utilized as factors for evaluating a process for producing an oxygen enriched gas by pressure swing adsorption
  • the nitrogen concentration is added thereto as a factor for evaluation.
  • the present invention is highly advantageous from the viewpoint of use of a mixed gas of oxygen and argon.
  • a product gas having a low nitrogen content i.e., 0.5% to 500 ppm
  • the product gas should be evaluated as a mixed gas which is composed of argon and oxygen, and evaluation should also be made in regard to the specific power consumption. Since argon gas is generally expensive, the product gas will be valued higher when evaluation is made with the cost thereof taken into consideration.
  • Another factor for evaluating a process may be the specific product (Nm3/H/m3), that is, the amount of oxygen produced per unit of time per unit amount of adsorbent. Evaluated in terms of this unit, a process which has a large value in terms of the specific product exhibits good performance and enable a reduction in the size of the apparatus.
  • the present invention is also superior in this point.
  • Three adsorption columns each having an inner diameter of 130 mm and a height of 2355 mm were prepared, and 21.8 kg of 5A type synthetic zeolite adsorbent in bead form having a diameter of 2.5 mm was charged in each column.
  • the nitrogen concentrations shown in Table 1 were measured by PID gas chromatography.
  • the designation "s.p.” represents the amount (Nm3) of product gas produced per unit of time per unit amount of adsorbent (m3), while "s.p.c.” (specific power consumption) represents an electric energy (KWH) required to generate 1 Nm3 c.o. of pure oxygen.
  • the second embodiment that is, a process wherein the recovery of the gas from the column in which the adsorp- tion step has already been completed, is effected through the feed ends of the two columns and through the effluent ends thereof at the same time, was tested in accordance with the above-described steps using three adsorption columns which were the same as those used in Example 1 and under the same running conditions as those in Example 1. The results of the experiment are shown in Table 2.
  • Table 4 compares the values for specific product and specific power consumption for obtaining product gases at 93% O2, 0.5% N2 and 0.1% N2, respectively, on the bases of the results of the experiments carried out in Examples 1 to 4 and comparative Examples 1 to 3.
  • "case” indicates "embodiment”.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
EP87311411A 1986-12-26 1987-12-23 Trennung eines mit Sauerstoff angereicherten Gases Withdrawn EP0273723A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP61313151A JPS63166702A (ja) 1986-12-26 1986-12-26 酸素ガス濃縮法
JP313151/86 1986-12-26

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EP0273723A2 true EP0273723A2 (de) 1988-07-06
EP0273723A3 EP0273723A3 (de) 1989-09-13

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0356861A2 (de) * 1988-09-01 1990-03-07 Bayer Ag Trennung von Gasgemischen durch Vakuum Swing Adsorption (VSA) in einem Zwei-Adsorber-System
FR2653355A1 (fr) * 1989-10-25 1991-04-26 Linde Kca Dresden Gmbh Procede pour separer les melanges gazeux par adsorption, par changement de pression.
EP0561340A1 (de) * 1992-03-17 1993-09-22 Kuraray Chemical Co., Ltd. Verfahren zur Abtrennung von Stickstoff-Gas
US5328503A (en) * 1992-11-16 1994-07-12 Air Products And Chemicals, Inc. Adsorption process with mixed repressurization and purge/equalization
EP0699467A3 (de) * 1994-09-01 1996-03-20 Praxair Technology Inc
EP0868936A1 (de) * 1997-04-02 1998-10-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Verfahren und Vorrichtung zur Trennung einer Gasmischung durch Adsorption

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Publication number Priority date Publication date Assignee Title
JP2562326B2 (ja) * 1987-08-07 1996-12-11 住友精化株式会社 空気から高濃度酸素を取得する方法
JP2683806B2 (ja) * 1988-03-17 1997-12-03 住友精化株式会社 濃縮酸素回収方法
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US4781735A (en) 1988-11-01
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JPS63166702A (ja) 1988-07-09

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